Process for hydrocarbon oil conversion



March 21, 1933. L. c. HUFF 1,901,969

PROCESS FOR HYDROCARBON OIL CONVERSION Filed Jan. 3. 1928 I m a Patented Mar. 21, 1933- UNITED STATES PATENT OFFICE ILYMAN G. HUFF, OF CHICAGO, ILLINOIS, ASSIGNOR T0 UNIVERSAL OIL PRODUCTS CO]!!- PANY, OF CHICAGO, ILLINOIS, A CORPORATION OF SOUTH DAKOTA PROCESS FOR BOCABBON OIL CONVERSION Application filed. January 3, 1928. Serial No. 244,108.

The present invention relates to improvements in process and apparatus for hydrocarbon oil conversion, and refers more particularly to a process and apparatus especially adapted for vapor phase cracking The invention has for its principal object the subjection of hydrocarbons to conditions of vapor phase cracking for the production of maximum yields of desirable lighter hydrocarbons therefrom'with a minimum production of coke and non-condensable gas loss. The invention has for another object the conversion of hydrocarbon oils under conditions of vapor phase cracking in such amanner that the condensed overhead product produced in the process will be suitable for use as motor fuel and will have high anti-knock properties, surpassing in this respect, the product of the present day liquid or liquidvapor phase processes.

T am aware that the art of conversion of hydrocarbons while subjecting same to conditions of vapor phase cracking is generally old. Heretofore, it has been diificult in cracking in the vapor phase, to properly heat the vapors. It is well known that vapors are hard to heat in any sort of container due to the poor heat conductivity, or rather, lack of conductivity, of vapors.

It is the purpose and one of the functions of the present invention to eliminate this dificulty, and the manner in which this is accomplished seems to be new and novel to the art.

In one of the preferred modes of carrying out the present invention,hydrocarbon oil vapors released froma concurrently operating distilling or cracking process are subjected to'conditions of temperature which cause conversion of said vapors in the vapor phase. This heat is imparted to the vapors by introducing a combustion supporting medium into contact with said vapors, causing a portion of the vapors to burn, thus producing hot gases of combustion which give ofi heat directly to the vapors. By this method the vapors may be heated and reacted within the same zone in a very economical and practical manner.

The utility of the invention as well as other objects, features, and advantages will be hereinafter more particularly apparent from the following detailed description.

The single figure in the drawing is a diagrammatic elevational view of the apparatus by which the objects of the present invention may be carried out.

Referring more in detail to the drawing, oil drawn from any suitable source may be forced by pump 1 through the line 2 and diverted into line 3 controlled by valve 4, or into line 5 controlled by valve 6 or both. That is, all or any regulated portion of the charge may be fed upwardly through the line 3 discharging into the dephlegmator 7 or all or any regulated-portion may be passed directly through the line 5 to the heating coil 8 mounted in a furnace 9. Assume for the purpose of this illustration that the oil is passed directly through the line 5 to the heating coil 8. While being passed through the latter, it is raised to conversion temperature, say 800 degrees F. more or less, passing out through the transfer line 10 controlled by valve 11 and discharging into the enlarged drum 12, which'may act as a separator and/or conversion drum. In the drum 12 the vaporous productsof reaction separate from the non-vaporous products, the vaporous products being released through the line, 13, controlled by valve 14, discharging into the chamber 15. The non-vaporous residue from the chamber 12 may be withdrawn through any of the drawoff lines 16, controlled by valves 17 and passed to storage.

A combustion supporting medium, such as air, may be drawn from a suitable source and forced by means of a pump 18 through line 19 into chamber 15. A pressure tank 20 and a valve 21 may be interposed in line 19. A portion of the hot vapors will spontaneously ignite as rapidly as the combustion supporting medium is injected into the chamber 15. It may be desirable to preheat the combustion supporting medium before introducing it into the vapors. This may be accomplished in an obvious manner. The hot combustion gases produced by the combustion of a part of the vapors will mix with the unburned vapors imparting their heat thereto to further their reaction. I

The non-vaporous residue from the chamber 15 may be withdrawn through the drawoif line 22 controlled by valve 23. The heated vapors after being given sufficient time to react may be passed from chamber 15 through line 24, controlled by valve 25, into the lower portion of dephlegmator 7. While ascending through the dephlegmator 7 the various products of reaction entering through line 24 are subjected to the action of a suitable cooling medium whereby the sufiiciently converted vaporous products remain uncondensed, passing out through the vapor outlet line 26 controlled by valve 27, being condensed in the condensing coil 28, the liquid being passed through the line 29 into the receiver 30. The receiver 30 may be provided with the usual liquid drawoff line 31, controlled by valve 32, and with the noncondensable gas relief line 33, controlled by valve 34.

Returning to the dephlegmator 7, the reflux condensate collecting in the bottom of the dephlegmator may be withdrawn through the line 35, and b means of the pump 36, passed through the ine 37 controlled by valve 38, merging with the line 5 whereby said. reflux condensate is returned to the heating coil 8 for retreatment. The cooling medium may be supplied to the-dephle mator by diverting all or a portion of the c arging stock from line 2 through line 3, or withdrawing a portion of the condensed distillate from the receiver 30 through line 39 and forcing it by means of the pump 40 through line 41 controlled by valve 42.

Under some conditions of operation it may be necessary to introduce into the vapors substantially undiluted oxygen instead of air.

It is to -be understood that any combustion supporting medium ma be used to support the combustion o the vapors within the chamber 15. It is obvious, of course, that by regulating the amount of air intgiduced into the vapors the amount of combustion'of the same may be controlled, as combustion will only take place to the extent of air admitted. Hence, the temperatures within chamber 15 can be very closely controlled, the va rs being heated to a temperature of 1000 egrees F., more or less, depending upon the production desired. This chamber may be suitably insulated to retain the heat imparted to the vapors.

The above described process ma be operated at atmospheric, subatmosp eric, or superatmospheric pressure, as may be desired.

Suitable safety devices can be installed to prevent excessive quantities of air bein introduced. The air pressure need only e a invention heavier constituents are withdrawn as a' liquid residue, passing the vapors so freed of heavier constituents to a zone of vapor phase cracking, and supplying heat for the vapor phase cracking by burmng a sufiicient amount of said vapors within said zone, to maintain a vapor phase cracking temperature.

In testimony whereof I aflix my si nature.

LYMAN C. H F. 

